CN101612511B - Micro-channel absorber for absorbing H2S - Google Patents
Micro-channel absorber for absorbing H2S Download PDFInfo
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- CN101612511B CN101612511B CN2008100120008A CN200810012000A CN101612511B CN 101612511 B CN101612511 B CN 101612511B CN 2008100120008 A CN2008100120008 A CN 2008100120008A CN 200810012000 A CN200810012000 A CN 200810012000A CN 101612511 B CN101612511 B CN 101612511B
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Abstract
The invention provides a micro-channel absorber, wherein a main body part is a plurality of micro-channels which are along the flow direction of gas and liquid, have certain mutual spacing distance and are applicable to receiving gas and liquid fluids; a contact mode of material flow between gas which needs to be absorbed and an absorption liquid is cocurrent; and an inlet of the absorber is provided with corresponding distribution devices of the gas and the liquid, which ensures the even distribution of the gas and the liquid. The micro-channel absorber has large gas treatment capacity in unit volume, and has a compact structure; and the micro-channel absorber is particularly suitable for removing acid gas (such as CO2, H2S and the like) in mixed gas flow such as synthetic gas, natural gas, coking gas, tail gas of coal gas, oilfield associated gas and Claus tail gas to reach the requirements of environmental emission and subsequent process gas processing.
Description
Technical field
The present invention relates to a kind of micro-channel absorber, can be particularly suitable for removing in the mixed airflows such as synthesis gas, natural gas, coking gas, coal gas tail gas, associated gas and Claus tail gas sour gas (as CO
2, H
2S etc.), to reach the required requirement of environmental emission and subsequent technique gas processing.
Background technology
Remove H at present
2The method of S is a lot, generally can be divided into dry desulfurization, wet desulphurization, embrane method desulfurization, biological desulphurization and desulfur technology that some are up-to-date.Wherein comparatively ripe with dry method and wet desulphurization.Dry desulfurization be with various adsorbents (as active carbon, molecular sieve, MnO, ZnO, Fe
2O
3Deng) adsorb H
2S, but dry method absorption is applicable to low concentration H
2The S mixed airflow, the occasion that high purified treatment requires, its adsorbents adsorb capacity is lower, and selectivity is little, is not suitable for handling the air-flow of high concentration, and floor space is big, and the regeneration energy consumption is big.The wet desulphurization method is big with its treating capacity, and operation is continuous, and absorption liquid can be regenerated, advantages such as investment and operating cost are low are widely used, wet desulphurization can be divided into the physics method, and the method that chemical method and physical chemistry combine is wherein with MDEA aqueous solution selectively removing H in the amine method
2The method of S is widely used.The packed tower of extensive use in Chemical Manufacture is at present still playing an important role; influence each other but exist between the two-phase fluid that contacts in the packed tower; usually can cause problems such as entrainment, liquid flooding, leakage, simultaneously huge packed tower volume makes that also the cost of operation and maintenance is higher.
Since the nineties in 20th century, little chemical industry technology is with its high mass transfer, high heat transfer, and simple in structure, characteristics such as no enlarge-effect and intrinsic safety develop rapidly at chemical field.The microreactor (micro-reactor) and traditional gas-liquid contanct equipment (wetted wall tower reactor of gas-liquid contact, bubbling column reactor, stir bubbling reactor, the sieve-plate tower absorber, the packed tower reactor, falling film reactor and spray reactor or the like) advantage of comparing: the gradient that reduces to increase physical quantity of (1) its linear-scale, thus increase motive force in the mass transport process, (2) surface area in the high specific area, common microreactor can reach 10000-50000m
2/ m
3Than the conventional laboratory and the big 2-3 of a specific area order of magnitude of industrial equipment, (3) volume reduces, because reducing and high specific area of linear-scale, the volume of microreactor sharply reduces even may diminish to several microlitres, reaction time shortens greatly, and has improved the security of equipment and the selectivity of course of reaction.
At present, must be before the large-scale natural gas line transportation through strict desulfurization and decarburization process.Rely on its low cost, high efficiency and integrated characteristics, microchannel absorption techniques and corollary equipment will have sizable competitive advantage in synthesis gas, natural gas, coking gas, coal gas tail gas, associated gas and Claus tail gas clean-up engineering.Micro-channel absorber is used for separating with the aspects such as GAS ABSORPTION of field of purification can realize that continuous high-efficient separates fast.Traditional amplification process is owing to exist enlarge-effect, and time and effort consuming generally needs 2-5.Because each passage is equivalent to an independently absorber in the micro-channel absorber, so amplification process promptly is the stack of number of active lanes, can save time, and reduces cost, and realizes the quick conversion of scientific achievement.
Summary of the invention
The object of the invention is to provide a kind of micro-channel absorber, and this micro-channel absorber can solve: one, improve the compactness of whole micro-channel absorber, the gas treatment amount of unit volume micro-channel absorber can reach 1 * 10
5m
3/ h/ (m
3The microchannel) more than; Two, reduce the resistance to mass tranfer of absorption process, improve mass-transfer efficiency; Three, thoroughly solve between the gas-liquid two-phase fluid that contacts in the conventional filler absorption tower influence each other, problem such as liquid flooding, leakage.
To achieve these goals, the technical solution used in the present invention is:
One, because microchannel efficiently, greatly improve the specific area of mass transfer, obtain very high mass transfer rate; The efficient heat transfer performance of microchannel makes that also interior each the interchannel temperature difference of micro-channel absorber is less; Two, liquid adopts the solid even distributor of liquid, gas distributor of gas employing and secondary air distributor, and gas-liquid two-phase distributes all very even; Three, adopt the gas-liquid way of contact of gas and liquid flowing, solved traditional problems such as entrainment, liquid flooding, leakage in the conventional filler absorption tower.
Technical scheme is specially:
A kind of absorption H
2The micro-channel absorber of S comprises the absorber body, is respectively arranged with lean solution in the absorber upper part of body and absorbs liquid inlet and gas tangent line inlet, be respectively arranged with the outlet of gas vent and rich absorption liquid in the bottom of absorber body; Be provided with the microchannel that is parallel to each other more than 2 or 2 in the middle part of the absorber body, the two ends of microchannel are provided with inlet public passage district and outlet public passage district;
Be provided with 1-5 in the gas access with inlet public passage interval and pass the gas distributor that connects layer by layer; Absorb the liquid inlet in lean solution and be provided with liquid distribution trough with inlet public passage interval; The equivalent diameter of described each microchannel can remove H according to the processing unstripped gas of concrete enforcement
2The requirement of S process and choosing, concrete scope is: 50 μ m-3000 μ m.
Described liquid distribution trough is the even distributor of liquid solid nozzle; The cross sectional shape of described microchannel is circle, triangle, wedge shape, square, rectangle, trapezoidal or sinusoidal etc.; The cross section of described whole micro-channel absorber can be designed to circle, square or rectangular etc.
The application of described micro-channel absorber, described micro-channel absorber is used for H
2The absorption process of S, its H in can the unstripped gas of purified treatment
2The S concentration range is wider: volumetric concentration 0.05%-10%.
When micro-channel absorber equipment moved, the scope of system pressure was selected wider: 0.1-5MPa, can select according to different embodiments.Absorbing temperature is 0-60 ℃, absorbs temperature and is preferably 0-30 ℃.
Absorb H in the unstripped gas
2The solvent of S can be selected according to specific embodiments, can be: monoethanolamine MEA, diethanol amine DEA, methyl diethanolamine MDEA, triethanolamine TEA, diglycolamine DGA or diisopropanolamine (DIPA) DIPA in the alcamines absorbent; Or the NHD NHD in the organic solvent; Propene carbonate, methyl alcohol, ethanol, polyethylene glycol or thiophane; Potash in the basic solvent or sodium carbonate liquor;
Or the mixed solvent formed of above more than one solvents.
Also be added with activator piperazine, diethylene glycol, imidazoles or methyl substituted imidazoles (for as 1-methylimidazole, glyoxal ethyline or 4-methylimidazole) in the described solvent.
Micro-channel absorber unit volume processing gas flow is big among the present invention, compact conformation; Be particularly suitable for removing in the mixed airflows such as synthesis gas, natural gas, coking gas, coal gas tail gas, associated gas and/or Claus tail gas sour gas (as CO
2, H
2S etc.), to reach environmental emission and the follow-up required requirement of process gas processing; The unstripped gas that is absorbed removes and comprises H
2Outside the S, also alternative other sour gas that absorbs in the unstripped gas is as CO
2Deng.
The gas of processing required for the present invention and absorption liquid pass through corresponding feed distributor respectively before entering the microchannel, and it is more even to distribute when it can make unstripped gas and material liquid enter the microchannel.Its main part is many microchannels that are suitable for holding the gas-liquid fluid along the certain space of having of Liquid Flow direction distance; The type of flow of logistics is concurrent flow between the gas of required processing and the absorption liquid; The absorber inlet has corresponding gas and distribution of liquid device, has guaranteed that gas and liquid evenly distribute in a plurality of microchannels of absorber.Each passage is equivalent to an independently absorber in the micro-channel absorber, and the stack by the microchannel number can obtain required more massive absorption plant.The field distribution of micro-channel absorber internal temperature is even.
The present invention is applied to H with micro-channel absorber first
2Removing of S mist can be with volume-diminished 1-2 of conventional filler tower more than the order of magnitude, and pressure reduction is less before and after the absorber, and having overcome in the past, packed tower takes off H
2Some drawbacks during S can reach the H more than 90% when low pressure (0.1-0.5MPa)
2The S removal efficiency, and the operating pressure of conventional filler tower is generally more than 5.0MPa.In addition, the cost of the investment of micro-channel absorber, operation and maintenance is all lower.
Description of drawings
Fig. 1 is the micro-channel absorber schematic diagram;
Fig. 2 is micro-channel absorber experiment flow figure in the specific implementation;
Fig. 3 is micro-channel absorber part of test results figure in the specific implementation.
The specific embodiment
Micro-channel absorber of the present invention (Fig. 1), a kind of absorption H
2The micro-channel absorber of S comprises the absorber body, is respectively arranged with lean solution in the absorber upper part of body and absorbs liquid inlet and gas tangent line inlet, be respectively arranged with the outlet of gas vent and rich absorption liquid in the bottom of absorber body; Be provided with the microchannel that is parallel to each other more than 2 or 2 in the middle part of the absorber body, the two ends of microchannel are provided with inlet public passage district and outlet public passage district; Be provided with 1-5 in the gas access with inlet public passage interval and pass the gas distributor that connects layer by layer; Absorb the liquid inlet in lean solution and be provided with liquid distribution trough with inlet public passage interval;
The equivalent diameter of described each microchannel can be chosen according to the requirement of the decarbonizing process of concrete enforcement, and concrete scope is: 50 μ m-3000 μ m.
Be mainly used in the mixed airflows such as removing synthesis gas, natural gas, coking gas, coal gas tail gas, associated gas and Claus tail gas sour gas (as CO
2, H
2S etc.), to reach environmental emission and the follow-up required requirement of process gas processing.Need take off H
2The unstripped gas that S purifies mainly comprises H
2S also can contain CO simultaneously
2Deng acid gas component, concrete composition has corresponding variation with the difference of actual demand application scenario.The absorbent that is used for micro-channel absorber can be selected: alcamines absorbent (MEA, DEA and MDEA), NHD (NHD), propene carbonate, methyl alcohol, ethanol, polyethylene glycol and thiophane, potash etc.Also can be the mixed solvent of above solvent composition, can also add a small amount of activator, the general activator that uses has: piperazine, diethylene glycol, imidazoles or methyl substituted imidazoles such as 1-methylimidazole, glyoxal ethyline, organic substances such as 4-methylimidazole.
The poor absorption liquid that is used for micro-channel absorber at first absorbs liquid inlet 11 through lean solution and enters, and evenly distributes in main body porch, microchannel through the solid even distributor 15 of liquid then.The H that contains that needs processing
2The unstripped gas of S is then entered by the gas tangent line of micro-channel absorber inlet 12, after gas distributor 13 and 14 twice distribution of secondary air distributor evenly downwards and lean solution absorption liquid contact.Gas-liquid two-phase by having many microchannels 18 of certain space distance, and is finished H in the cocurrent cooling operation mode in microchannel 18
2The absorption process of S.Purge gas enters next operation by gas vent 16, and rich absorption liquid enters regenerator regeneration by rich absorption liquid outlet 17.The cross section of whole micro-channel absorber can be designed as circle 19, also can be designed to square, rectangle or other geometries according to the actual requirements.
Micro-channel absorber of the present invention experiment flow is in the specific implementation seen Fig. 2.During experiment, at first unstripped gas 20 and poor absorption liquid 28 are entered micro-channel absorber 24 according to a certain percentage, the amount of unstripped gas 20 and lean solution absorption liquid 28 is respectively by mass flowmenter 21 and pump 23a control.Unstripped gas also needs to be preheating to by preheater 22a temperature required before entering micro-channel absorber 24, and poor absorption liquid needs preheater 22b first preheating before entering micro-channel absorber 24 too.Unstripped gas and is finished absorption process in micro-channel absorber 24 and flow through microchannel group in the micro-channel absorber 24 of poor absorption liquid and stream, and Purge gas 29 enters subsequent processing by 16 outflows of ad hoc gas vent.Rich solution then enters regenerator 25 regeneration by rich absorption liquid outlet 17, obtains the H of higher concentration
2S gas 30.Flow through heat exchanger 22c and annotate back poor absorption liquid storage tank by pump 23b and recycle fully of poor absorption liquid after the regeneration.In addition, Pressure gauge 26a from flow chart and 26b can know that the pressure drop of whole micro-channel absorber 24 changes between the 0-0.05MPa with not coexisting for the treatment of capacity.Also be provided with the thief hatch 27a and the 27b of unstripped gas and rich absorption liquid in the concrete flow process of implementing respectively.
In order to be briefly described the certain situation in the actual implementation process, now select the aqueous solution absorption of MDEA to contain 1200ppm H
2The mist of S illustrates.Part of test results is seen Fig. 3.
Manufactured and designed serial 1-10m by above-mentioned design
3The micro-channel absorber of/h gas treatment amount, the treating capacity of micro-channel absorber has reached 1 * 10
5m
3/ h/ (m
3The microchannel) more than.According to different technological requirements, can adopt the ratio of different unstripped gas and absorbent, H in the purified gas
2S can drop to 0-100ppm by 1200ppm, and this depends on the requirement of user to the purified gas quality fully.When low pressure (0.1-0.5MPa), can reach the H more than 90%
2The S removal efficiency,
Micro-channel absorber of the present invention both can be widely used in the mixed airflows such as removing synthesis gas, natural gas, coking gas, coal gas tail gas, associated gas and Claus tail gas sour gas (as CO
2, H
2S etc.), to reach environmental emission and the follow-up required requirement of process gas processing.The scale of the processing unstripped gas of micro-channel absorber can be by 1000-100000m
3/ h, bigger scale also can be realized by identical micro-channel absorber combination.
Claims (10)
1. one kind absorbs H
2The micro-channel absorber of S comprises the absorber body, is respectively arranged with lean solution in the absorber upper part of body and absorbs liquid inlet (11) and gas tangent line inlet (12), be respectively arranged with gas vent (16) and rich absorption liquid in the bottom of absorber body and export (17); It is characterized in that: be provided with the microchannel that is parallel to each other (18) more than 2 or 2 at absorber body middle part, the two ends of microchannel (18) are provided with inlet public passage district and outlet public passage district;
(12) are provided with 1-5 with inlet public passage interval and pass the gas distributor that connects layer by layer in the gas access; Absorb liquid inlet (11) in lean solution and be provided with liquid distribution trough with inlet public passage interval; The equivalent diameter of described each microchannel (18) is: 50 μ m-3000 μ m.
2. according to the described micro-channel absorber of claim 1, it is characterized in that: described liquid distribution trough is the even distributor of liquid solid nozzle.
3. according to the described micro-channel absorber of claim 1, it is characterized in that: the cross sectional shape of described microchannel is circle, triangle, rectangle or trapezoidal.
4. according to the described micro-channel absorber of claim 1, it is characterized in that: the cross section of described whole micro-channel absorber can be designed to circle or rectangle.
5. the application of the described micro-channel absorber of claim 1 is characterized in that: described micro-channel absorber is used for H
2The absorption process of S, the H in the unstripped gas of its purified treatment
2S volumetric concentration 0.05%-10%.
6. according to the described application of claim 5, it is characterized in that: during the micro-channel absorber operation, it is 0-60 ℃ that system pressure: 0.1-5MPa absorbs temperature
7. according to the described application of claim 5, it is characterized in that: absorb H in the unstripped gas
2The solvent of S is: monoethanolamine MEA, diethanol amine DEA, methyl diethanolamine MDEA, triethanolamine TEA, diglycolamine DGA or diisopropanolamine (DIPA) DIPA in the alcamines absorbent; Or the NHD NHD in the organic solvent; Propene carbonate, methyl alcohol, ethanol or polyethylene glycol; Potash in the basic solvent or sodium carbonate liquor;
Or the mixed solvent formed of above solvent.
8. according to the described application of claim 7, it is characterized in that: also be added with activator piperazine, diethylene glycol, imidazoles or methyl substituted imidazoles in the described solvent.
9. according to the described application of claim 8, it is characterized in that: described methyl substituted imidazoles is 1-methylimidazole, glyoxal ethyline or 4-methylimidazole.
10. according to the described application of claim 5, it is characterized in that: described micro-channel absorber is suitable for removing sour gas in synthesis gas, natural gas, coking gas, coal gas tail gas, associated gas and/or the Claus tail gas air-flow, to reach environmental emission and the follow-up required requirement of process gas processing; The unstripped gas that is absorbed removes and comprises H
2Outside the S, also alternative other sour gas that absorbs in the unstripped gas.
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|---|---|---|---|
| CN2008100120008A CN101612511B (en) | 2008-06-25 | 2008-06-25 | Micro-channel absorber for absorbing H2S |
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| CN2008100120008A CN101612511B (en) | 2008-06-25 | 2008-06-25 | Micro-channel absorber for absorbing H2S |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102836631A (en) * | 2012-09-13 | 2012-12-26 | 上海华畅环保设备发展有限公司 | Method and device for selectively removing hydrogen sulfide from gas by utilizing amine droplets |
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| JP5713997B2 (en) * | 2010-03-29 | 2015-05-07 | 株式会社東芝 | Acid gas absorbent, acid gas removal device, and acid gas removal method |
| CN102784543B (en) * | 2011-05-17 | 2014-09-03 | 中国科学院大连化学物理研究所 | Fractal micro channel reactor system for enhancing CO2 absorption, and method thereof |
| CN103463958B (en) * | 2013-09-24 | 2015-12-23 | 北京化工大学 | Utilize membrane dispersion type micro-channel reactor selective absorbing containing CO 2h in mist 2the method of S |
| CN104147897A (en) * | 2014-07-21 | 2014-11-19 | 宜兴市星光宝亿化工有限公司 | DGA composite total sulfur removal agent used in petrochemical industry and preparation method of DGA composite total sulfur removal agent |
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| CN105344205A (en) * | 2014-08-20 | 2016-02-24 | 中国石油化工股份有限公司 | Absorber for selectively removing H2S from CO2-containing mixing gas |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1266733A (en) * | 1999-03-10 | 2000-09-20 | 日本派欧尼股份株式会社 | Process and apparatus for recovery of ammonia |
| CN2475459Y (en) * | 2000-12-27 | 2002-02-06 | 程培胜 | Tower tray type overall sucking tower |
| CN1767888A (en) * | 2002-10-30 | 2006-05-03 | 万罗赛斯公司 | Process for separating a fluid component from a fluid mixture by sorption using microchannel process technology |
-
2008
- 2008-06-25 CN CN2008100120008A patent/CN101612511B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1266733A (en) * | 1999-03-10 | 2000-09-20 | 日本派欧尼股份株式会社 | Process and apparatus for recovery of ammonia |
| CN2475459Y (en) * | 2000-12-27 | 2002-02-06 | 程培胜 | Tower tray type overall sucking tower |
| CN1767888A (en) * | 2002-10-30 | 2006-05-03 | 万罗赛斯公司 | Process for separating a fluid component from a fluid mixture by sorption using microchannel process technology |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102836631A (en) * | 2012-09-13 | 2012-12-26 | 上海华畅环保设备发展有限公司 | Method and device for selectively removing hydrogen sulfide from gas by utilizing amine droplets |
| CN102836631B (en) * | 2012-09-13 | 2014-09-24 | 上海华畅环保设备发展有限公司 | Method and device for selectively removing hydrogen sulfide from gas by utilizing amine droplets |
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